US20080019884A1 - Apparatus for Producing Hydrogen - Google Patents

Apparatus for Producing Hydrogen Download PDF

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Publication number
US20080019884A1
US20080019884A1 US10/581,582 US58158204A US2008019884A1 US 20080019884 A1 US20080019884 A1 US 20080019884A1 US 58158204 A US58158204 A US 58158204A US 2008019884 A1 US2008019884 A1 US 2008019884A1
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US
United States
Prior art keywords
stage
producing hydrogen
methanization
flow
hydrogen according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/581,582
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English (en)
Inventor
Nicolas Zartenar
Peter Britz
Klaus Wanninger
Anja Wick
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Viessmann Werke GmbH and Co KG
Sued Chemie AG
Original Assignee
Viessmann Werke GmbH and Co KG
Sued Chemie AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Viessmann Werke GmbH and Co KG, Sued Chemie AG filed Critical Viessmann Werke GmbH and Co KG
Assigned to SEUD-CHEMIE AG, VIESSMANN WERKE GMBH & CO. KG reassignment SEUD-CHEMIE AG ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WICK, ANJA, WANNINGER, KLAUS, ZARTENAR, NICOLAS, BRITZ, PETER
Assigned to SUED-CHEMIE AG, VIESSMANN WERKE GMBH & CO. KG reassignment SUED-CHEMIE AG CORRECTIVE ASSIGNMENT TO CORRECT THE TYPOGRAPHICAL ERROR IN THE SPELLING OF THE SECOND ASSIGNEE'S NAME PREVIOUSLY RECORDED ON REEL 019076 FRAME 0817. ASSIGNOR(S) HEREBY CONFIRMS THE CORRECT SPELLING OF THE SECOND ASSIGNEE'S NAME IS: SUED-CHEMIE AG. Assignors: WICK, ANJA, WANNINGER, KLAUS, ZARTENAR, NICOLAS, BRITZ, PETER
Publication of US20080019884A1 publication Critical patent/US20080019884A1/en
Abandoned legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
    • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/586—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being a methanation reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/0445—Selective methanation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0816—Heating by flames
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling

Definitions

  • the present invention relates to an apparatus for producing hydrogen according to the preamble of claim 1 .
  • This apparatus comprises, inter alia, a steam reformer stage, preferably heatable using a burner, for converting hydrocarbon gas and water into hydrogen and further reformer products such as carbon dioxide and carbon monoxide.
  • a steam reformer stage preferably heatable using a burner
  • reformer products such as carbon dioxide and carbon monoxide.
  • a PEM fuel cell may be operated using the hydrogen produced. Since the reformate still contains a comparatively large amount of carbon monoxide after the reformer stage (fuel-cell poison), a catalyst stage is connected downstream therefrom, in order to catalytically convert the carbon monoxide into carbon dioxide (unproblematic for the fuel cell).
  • a methanization stage is connected downstream from the catalyst stage, which converts the remaining carbon monoxide (back) into methane gas using hydrogen.
  • the entry temperature of the reformate gas containing the carbon monoxide into the methanization stage is typically approximately 240° C. in this case. Since the methanization process proceeds exothermically, cooling of the methanization stage is necessary.
  • a flow guiding housing for a coolant is provided, which is assigned to the stage alternately externally or from the interior (for hollow-cylindrical implementation, for example), depending on the implementation of the methanization stage. This flow guiding housing may have the coolant flow through it in parallel flow or counterflow to the reformate flow as needed.
  • the present invention is accordingly based on the object of ensuring in the simplest possible way, in an apparatus of the type cited at the beginning, that this retroshift reaction does not occur and the carbon monoxide component in the reformate gas at the outlet of the methanization stage is as low as possible, preferably significantly less than 100 ppm.
  • the flow guiding housing has at least two, preferably three or more cooling zones having different cooling effects situated one behind another in the axial direction.
  • the use of at least two cooling zones results in a stepped or continuously changing temperature curve within the methanization stage—depending on the constructive implementation of the cooling zones—which in turn results, with corresponding coolant temperature, in the temperature being reduced significantly toward the exit of the methanization stage in spite of the exothermic methanization process and the undesired retroshift reaction accordingly not occurring.
  • the special advantage of the present invention is thus that the temperature curve within the methanization stage may be influenced in a targeted way and a minimal carbon monoxide content in the reformate gas may be achieved in this way.
  • an “air bleed” may also be dispensed with in this case, which until now was connected downstream from the methanization stage and upstream from the fuel cell, and in which the residual carbon monoxide contained in the reformate was oxidized using small quantities of oxygen.
  • FIG. 1 schematically shows the apparatus according to the present invention having a methanization stage having four cooling zones in section;
  • FIG. 2 shows the temperature curve as a diagram plotted over the run length x within the methanization stage when one cooling zone is used (related art);
  • FIG. 3 shows the temperature curve as a diagram plotted over the run length x within the methanization stage when four cooling zones are used;
  • FIG. 4 shows the temperature curve as a diagram plotted over the run length x within the four cooling zones
  • FIG. 5 schematically shows two further embodiments of the flow guiding housing on the methanization stage in section (summarized in one illustration for the sake of simplicity);
  • FIG. 6 schematically shows a further embodiment of the flow guiding housing on the methanization stage in section.
  • FIG. 1 schematically shows the apparatus according to the present invention for producing hydrogen in section.
  • the reformer stage 1 for converting hydrocarbon gas and water into hydrogen and further reformer products.
  • the reformer stage 1 which has a reformer catalyst, is preferably implemented, as shown, as a steam reformer stage heated using a burner 9 , in particular a gas burner, i.e., in this stage, for example, CH 4 and H 2 O are converted into CO, CO 2 , and H 2 while heat is supplied (by the burner 9 ) (endothermic reaction).
  • the reformer stage 1 is preferably implemented as a hollow cylinder, as shown.
  • the apparatus according to the present invention comprises at least one catalyst stage 2 , connected downstream from the reformer stage 1 , for catalytic conversion of the carbon monoxide, i. e., this is at least partially converted into carbon dioxide, which is harmless to the fuel cell.
  • the catalyst stage 2 is advantageously also implemented as a hollow cylinder. This measure results in a more uniform temperature curve and thus in better carbon monoxide conversion within the catalyst stage 2 .
  • the apparatus comprises a methanization stage 3 connected downstream from the catalyst stage 2 , which has axial flow through it and which, as noted, is used for the purpose of methanizing as much as possible of the residual carbon monoxide contained in the reformate gas using hydrogen.
  • a flow guiding housing 4 for a coolant which extends in the axial flow direction, is assigned thereto.
  • the methanization stage 3 is preferably also implemented as a hollow cylinder, as shown.
  • the reformer stage 1 , the catalyst stage 2 , and the methanization stage 3 are situated one after another in the axial flow direction.
  • the stages are also advantageous for the stages to be situated one after another defining a continuous annular chamber in the axial flow direction.
  • the flow guiding housing 4 has at least two, preferably three or more cooling zones 5 , 6 , 7 , 8 having different cooling effects situated one after another in the axial direction.
  • the flow guiding housing 4 is divided into four cooling zones 5 , 6 , 7 , 8 , to each of which the coolant may be supplied separately.
  • two zones are already capable of achieving the object defined at the beginning. The more cooling zones are provided, the more precisely may the temperature curve within the methanization stage be fixed, but the outlay for apparatus also becomes greater. Four zones have been shown to be a favorable selection here.
  • the cooling zones 5 , 6 , 7 , 8 With a hollow-cylindrical implementation of the methanization stage 3 , it has also been shown to be advantageous for the cooling zones 5 , 6 , 7 , 8 to be situated alternately inside and/or outside the methanization stage 3 (see FIG. 6 ).
  • the cooling zones 5 , 6 , 7 , 8 preferably enclose the methanization stage 3 like annular chambers situated axially one after another or, with a hollow-cylindrical implementation of the methanization stage 3 , are enclosed thereby (see FIG. 6 again).
  • each cooling zone 5 , 6 , 7 , 8 it is also advantageous for each cooling zone 5 , 6 , 7 , 8 to have at least one coolant supply connection 10 and one coolant removal connection 11 , each cooling zone 5 , 6 , 7 , 8 additionally advantageously being able to have coolant flow through it alternately in parallel flow (not shown) or in counterflow to the methanization stage 3 .
  • FIG. 2 shows a temperature curve over the run length x (see FIG. 1 ) within a methanization stage, which only has one cooling zone (related art).
  • carbon monoxide and hydrogen is converted back into hydrocarbon gas (methane) in the methanization stage in order to reduce the carbon monoxide component in the reformate gas.
  • methane hydrocarbon gas
  • the temperature first rises in the stage and then falls because of the cooling to a value just below the entry temperature.
  • the carbon monoxide content is typically approximately 120 ppm, i.e., too much to conduct the reformate gas directly to the fuel cell.
  • an “air bleed” is therefore typically connected downstream from the methanization stage in order to also remove this component of carbon monoxide.
  • the methanization stage is divided into multiple cooling zones in order to lower the temperature toward the outlet of the stage in a targeted way so that the undesired retroshift reactions no longer occur.
  • a corresponding temperature curve is shown in FIG. 3 , which may be implemented if the cooling zone distribution according to the present invention is used.
  • the temperature in the methanization stage thus falls with this achievement of the object continuously from 240° C. to approximately 220° C., with the result that, in particular at the end of the methanization stage, retroshift reactions may no longer occur, since the temperatures are too low for this purpose in the area of this cooling zone.
  • the reference numbers 5 , 6 , 7 , 8 and the dotted lines in FIG. 3 are to illustrate the area where the cooling zones are situated.
  • FIG. 4 illustrates the temperature curve within the individual cooling zones. It is particularly noticeable that because of the cooling in counterflow, a type of sawtooth profile arises, but the temperature peaks always fall again toward the outlet of the stage, from which the desired, falling temperature curve within the methanization stage may necessarily be concluded.
  • the cooling zones 5 , 6 , 7 , 8 situated one behind another in the axial direction are directly hydraulically connected to one another, but have different flow cross-sections.
  • a direct hydraulic separation of the cooling zones 5 , 6 , 7 , 8 is not required, rather the heat transmission in the individual areas of the methanization stage may also be influenced in a targeted way through suitable selection of the axial flow cross-sections.
  • a large flow cross-section means a low flow speed and therefore relatively poor heat transmission
  • a small cross-section means a high flow speed and therefore quite good heat transmission; all also as a function of temperature gradient between coolant and methanization stage, of course.
  • cooling zones 5 , 6 , 7 , 8 have stepped flow cross-sections to one another in the axial direction.
  • continuously changing flow cross-sections are also provided, in both cases the cooling zones 5 , 6 , 7 , 8 alternately being able to have coolant flow through them in parallel flow or counterflow to the methanization stage 3 .

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
US10/581,582 2003-12-02 2004-11-25 Apparatus for Producing Hydrogen Abandoned US20080019884A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10356650A DE10356650A1 (de) 2003-12-02 2003-12-02 Apparat zur Erzeugung von Wasserstoff
DE10356650.3 2003-12-02
PCT/DE2004/002608 WO2005054125A1 (de) 2003-12-02 2004-11-25 Apparat zur erzeugung von wasserstoff

Publications (1)

Publication Number Publication Date
US20080019884A1 true US20080019884A1 (en) 2008-01-24

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US10/581,582 Abandoned US20080019884A1 (en) 2003-12-02 2004-11-25 Apparatus for Producing Hydrogen

Country Status (5)

Country Link
US (1) US20080019884A1 (de)
EP (1) EP1651563A1 (de)
JP (1) JP2007513044A (de)
DE (1) DE10356650A1 (de)
WO (1) WO2005054125A1 (de)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5037878B2 (ja) * 2006-08-25 2012-10-03 日本碍子株式会社 選択透過膜型反応器及び水素ガスの製造方法
US8709668B2 (en) * 2010-08-03 2014-04-29 Panasonic Corporation Hydrogen generation device and fuel cell system
JP6194143B2 (ja) * 2013-09-09 2017-09-06 千代田化工建設株式会社 水素及び合成天然ガスの製造装置及び製造方法
KR101850268B1 (ko) * 2013-09-09 2018-04-20 치요다가코겐세츠가부시키가이샤 수소 및 합성 천연가스의 제조 장치 및 제조 방법

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3441393A (en) * 1966-01-19 1969-04-29 Pullman Inc Process for the production of hydrogen-rich gas
US6403049B1 (en) * 1997-09-25 2002-06-11 Johnson Matthey Public Limited Company Hydrogen purification
US20030035983A1 (en) * 1999-12-28 2003-02-20 Kunihiro Ukai Power generation device and operation method therefor
US6632409B1 (en) * 1998-12-21 2003-10-14 Aisin Seiki Kabushiki Kaisha Reformer for fuel cell system
US20050172553A1 (en) * 2002-03-25 2005-08-11 Nicolas Zartenar Device for the generation of hydrogen

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Publication number Priority date Publication date Assignee Title
DE10213326A1 (de) * 2002-03-25 2003-10-16 Viessmann Werke Kg Apparat zur Erzeugung von Wasserstoff
GB9713474D0 (en) * 1997-06-27 1997-09-03 Johnson Matthey Plc Catalytic reactor
JP3723680B2 (ja) * 1998-03-05 2005-12-07 三洋電機株式会社 Ｃｏ除去装置およびｃｏ除去装置の運転方法
JP2000256003A (ja) * 1999-03-08 2000-09-19 Osaka Gas Co Ltd 水素リッチガス中のｃｏ除去方法
JP3772619B2 (ja) * 1999-12-28 2006-05-10 松下電器産業株式会社 水素発生装置
DE10057537A1 (de) * 2000-11-20 2002-06-06 Viessmann Werke Kg Apparat zur Erzeugung von Wasserstoff
EP1350071B1 (de) * 2000-12-13 2013-04-03 Texaco Development Corporation Kompakte brennstoffbehandlungsvorrichtung mit einer kammer
JP2002282690A (ja) * 2001-03-26 2002-10-02 Osaka Gas Co Ltd 一酸化炭素除去用触媒および一酸化炭素除去方法ならびに一酸化炭素除去反応器
JP3853632B2 (ja) * 2001-10-26 2006-12-06 三菱電機株式会社 燃料電池発電装置用一酸化炭素除去器及び運転方法
EP1486456B1 (de) * 2002-03-15 2010-06-02 Panasonic Corporation Reformiervorrichtung und betriebsverfahren dafür
JP2003277013A (ja) * 2002-03-27 2003-10-02 Osaka Gas Co Ltd 一酸化炭素除去方法及び固体高分子型燃料電池システム
DE10250793A1 (de) * 2002-10-30 2004-05-19 Viessmann Werke Gmbh & Co Kg Apparat zur Erzeugung von Wasserstoff und Verfahren zum Betrieb eines solchen Apparats

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3441393A (en) * 1966-01-19 1969-04-29 Pullman Inc Process for the production of hydrogen-rich gas
US6403049B1 (en) * 1997-09-25 2002-06-11 Johnson Matthey Public Limited Company Hydrogen purification
US6632409B1 (en) * 1998-12-21 2003-10-14 Aisin Seiki Kabushiki Kaisha Reformer for fuel cell system
US20030035983A1 (en) * 1999-12-28 2003-02-20 Kunihiro Ukai Power generation device and operation method therefor
US20050172553A1 (en) * 2002-03-25 2005-08-11 Nicolas Zartenar Device for the generation of hydrogen

Also Published As

Publication number Publication date
EP1651563A1 (de) 2006-05-03
DE10356650A8 (de) 2005-12-01
JP2007513044A (ja) 2007-05-24
WO2005054125A1 (de) 2005-06-16
DE10356650A1 (de) 2005-07-07

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Owner name: VIESSMANN WERKE GMBH & CO. KG, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ZARTENAR, NICOLAS;BRITZ, PETER;WANNINGER, KLAUS;AND OTHERS;REEL/FRAME:019076/0817;SIGNING DATES FROM 20070124 TO 20070320

Owner name: SEUD-CHEMIE AG, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ZARTENAR, NICOLAS;BRITZ, PETER;WANNINGER, KLAUS;AND OTHERS;REEL/FRAME:019076/0817;SIGNING DATES FROM 20070124 TO 20070320

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Owner name: VIESSMANN WERKE GMBH & CO. KG, GERMANY

Free format text: CORRECTIVE ASSIGNMENT TO CORRECT THE TYPOGRAPHICAL ERROR IN THE SPELLING OF THE SECOND ASSIGNEE'S NAME PREVIOUSLY RECORDED ON REEL 019076 FRAME 0817;ASSIGNORS:ZARTENAR, NICOLAS;BRITZ, PETER;WANNINGER, KLAUS;AND OTHERS;REEL/FRAME:019142/0415;SIGNING DATES FROM 20070124 TO 20070320

Owner name: SUED-CHEMIE AG, GERMANY

Free format text: CORRECTIVE ASSIGNMENT TO CORRECT THE TYPOGRAPHICAL ERROR IN THE SPELLING OF THE SECOND ASSIGNEE'S NAME PREVIOUSLY RECORDED ON REEL 019076 FRAME 0817;ASSIGNORS:ZARTENAR, NICOLAS;BRITZ, PETER;WANNINGER, KLAUS;AND OTHERS;REEL/FRAME:019142/0415;SIGNING DATES FROM 20070124 TO 20070320

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